Apparatus and process for the production of soda ash

ABSTRACT

A device and process for the separate removal of oppositely charged ions from electrolyte solutions and recombining them to form new chemical compositions. The invention provides the ability to create multiple ion flow channels and then form new chemical compositions therefrom. The process is accomplished by selectively combining oppositely charged ions of choice from different electrolyte solutions via the capacitive behavior of high electrical capacitance electrodes confined in insulated containers. Industrial plants employing the inventive process can have the flexibility to produce needed industrial chemical compounds such as Soda Ash, Caustic Soda, hydrochloric acid and chlorine gas, based on market demand, and can be located near points of consumption to significantly reduce transportation costs.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional application of U.S. application Ser.No. 15/700,794 filed Sep. 11, 2017, the disclosure of which isincorporated herein by reference in its entirety.

FIELD OF THE INVENTION

The present invention relates to the separation and selectiverecombination of ions from differing electrolyte solutions to produceuseful chemical compounds, and compounds which have limited occurrencein nature, such as soda ash.

BACKGROUND OF THE INVENTION

There are many chemical compounds which must be manufactured throughspecial chemical processes. Such compounds are typically useful forvarious industrial purposes worldwide, but have only a limitedoccurrence in nature. The synthesis of these compounds typicallyrequires a large number of steps, a large amount of energy, and theformation of intermediate by-products that are often of low value or areuseless or even harmful to the environment. Therefore, in order toreduce energy consumption and the number of intermediate steps neededprior to reaching a final product, it would be advantageous in theindustrial chemical arts to provide simplified synthesis processes forvarious useful chemical compounds.

Presently three industrial processes are used for manufacturing sodiumcarbonate (i.e. Soda Ash). The Solvay process uses limestone (calciumcarbonate, CaCO₃) and salt brine (sodium chloride, NaCl) as rawmaterials, and ammonia (NH₃) as an intermediary, and is the prevailingprocess used in Europe and many other regions. The overall chemicalequation for the Solvay Process can be written as:

CaCO₃+2NaCl→Na₂CO₃+CaCl₂   (Equation 1)

However, in order to reach the end products, the Solvay process involvesmany intermediate steps. First, calcium carbonate (limestone) is heatedto release carbon dioxide:

CaCO₃→CaO+CO₂   (Equation 2)

The remainder of the process is centered about a large hollow tower. Atthe top of the tower, a concentrated solution of sodium chloride andammonia enter the tower. As the carbon dioxide bubbles up through thissolution, sodium bicarbonate is produced and precipitates according tothe following equation:

NaCl+NH₃+CO₂+H₂O→NaHCO₃+NH₄Cl   (Equation 3)

The sodium bicarbonate, separated by filtration, is then converted tosodium carbonate by heating it, which also releases water and carbondioxide:

2NaHCO₃→Na₂CO₃+H₂O+CO₂   (Equation 4)

Calcium hydroxide is then produced by reacting the calcium oxidegenerated in Equation 2 with water:

CaO+H₂O→Ca(OH)₂   (Equation 5)

From here, the ammonium chloride produced in Equation 3 is treated withthe calcium hydroxide produced in Equation 5 mainly to recover theammonia which is recycled:

Ca(OH)₂+2NH₄Cl→CaCl₂+2NH₃+2H₂O   (Equation 6)

In addition to producing Soda Ash (i.e. sodium carbonate, see Equation4), the Solvay process also generates calcium chloride as a by-product(see Equation 6). While calcium chloride has a number of uses, mostnotably as a road de-icing agent, typically the manufacturers of SodaAsh have a major issue disposing of this by-product. For example, inseaside locations such as Saurashtra, Gujarat, India, excess calciumchloride is deposited into the sea; or in Osborne, South Australia,after it was observed that calcium chloride was silting up the shippingchannel, the practice of dumping it into a settling pond was adopted.

Another well-known process for manufacturing sodium carbonate is Hou'sprocess. This process is advantageous where a supply of carbon dioxideis available but sources of limestone (i.e. calcium carbonate) aredistant. In this process carbon dioxide (produced by such processes assteam reforming) is passed through a nearly saturated solution of sodiumchloride and ammonia, much like the Solvay process (see Equation 3,above). However, after removal of the precipitated sodium bicarbonate(NaHCO₃), the remaining solution is cooled to allow the precipitation ofammonium chloride (NH₄Cl), which can be sold as a fertilizer afterremoval from the cooled solution. Because the ammonia and sodiumchloride need to be replenished, Hou process plants need to be locatednear ammonia production facilities.

In the United States, the discovery in Wyoming and California of majorsodium carbonate deposits in the form of the mineral Trona has led tothe gradual replacement of synthetic Soda Ash production, partially inan effort to lessen the environmental impact of calcium chloride (fromindustrial Solvay process plants) polluting the ground water at plantsite landfills. There are also Trona mines in Turkey and in Lake Magadiin Kenya. Purified Soda Ash produced by refining mined Trona ore can beshipped to paper and glass factories and for use in various chemical andpetrochemical plants. For example, purified Soda Ash is typicallyshipped from mines in Wyoming and California to eastern and southernU.S. states, mostly by rail.

While the mining of Trona ore is one solution to syntheticallymanufacturing Soda Ash, the economic cost of transporting the purifiedSoda Ash across the country becomes a major consideration. And whilesynthesizing Soda Ash locally would be the preferred solution, currentsynthesis processes such as the Solvay process have their own economicand environmental problems, associated with the supply of reactants andthe disposal of by-product calcium chloride and the economics of thescale requiring rather large plants to produce soda ash using the Solvayprocess.

In light of the above, it is apparent that there is a need in the artfor a more economically and environmentally friendly process for theproduction of Soda Ash. U.S. Pat. Nos. 8,715,477, 9,309,133 and9,315,398, which are all by the current inventor A. Yazdanbod and areincorporated herein by reference in their entireties, teach processesand devices for Ion Separation and Recomposition Technology (ISART).ISART involves synthesizing new chemical compounds that traditionallyhave been hard to construct, by exchanging oppositely charged ions fromone chemical compound for those of another. The ISART inventionsdescribed in the patents listed above can also be used for desalinationof water by selective removal and depletion of ions. With ISART, in itsmany variations, it is now possible to separately remove charged ionsfrom a first electrolyte solution and selectively recombine thesecharged ions with oppositely charged ions from a second electrolytesolution to form new chemical compositions in one or two steps.

In light of the above discussion regarding the production of Soda Ash,it would be advantageous to employ certain applications of ISARTtechnology to produce needed industrial chemical compounds such as SodaAsh. It would also be advantageous to provide a chemical productionprocess for Soda Ash which uses less energy than current Solvay or Houprocesses and does not include the production of calcium chloride. Itwould likewise be useful if an industrial plant producing Soda Ash hasno by-products requiring disposal. It would further be advantageous ifan industrial plant producing Soda Ash can be located near points ofconsumption, to significantly reduce transportation costs. It would alsobe useful if such a plant could have flexible production capabilities toadjust to varying market demands. It would further be advantageous ifthe polluting and greenhouse gas carbon dioxide could be utilized by anovel process to produce Soda Ash.

SUMMARY OF THE INVENTION

Accordingly, the present invention relates to improvements in theapparatuses and methods used and patented by the present inventor forIon Separation and Recomposition Technology (ISART). The invention alsorelates to a novel approach for the production of Soda Ash (i.e. sodiumcarbonate) using the ISART process. Industrial plants employing theISART process can have the flexibility to produce needed industrialchemical compounds such as Soda Ash, Caustic Soda, hydrochloric acid andchlorine gas, based on market demand, and can be located near points ofconsumption to significantly reduce transportation costs.

A first aspect of the invention is a process for capacitive generationof ion streams, comprising: (a) providing a first electrolyte solutionin a first hydraulically isolated section and a second electrolytesolution in a second hydraulically isolated section, wherein eachelectrolyte solution comprises positive ions and negative ions; (b)separating the positive ions from the negative ions in each of the firstand second electrolyte solutions, wherein separating comprises the stepsof: (i) placing a first EDLC electrode inside the first electrolytesolution; (ii) placing a second EDLC electrode inside the secondelectrolyte solution; and (iii) applying an electric potentialdifference between the EDLC electrodes such that two capacitors inseries are formed in each of the first and second electrolyte solutions;(c) electrically drawing the ions out of each of the first and secondelectrolyte solutions as oppositely charged ion streams, wherein thepositive and negative ion streams are generated in a continuous fashionand are selectively drawn through an ion selective membrane selective tothe ion stream; and (d) pooling the ion stream from the firstelectrolyte solution and the oppositely charged ion stream from thesecond electrolyte solution into a third hydraulically isolated sectionwith sides made up of the ion selective membranes of the first and thesecond hydraulically isolated sections.

A second aspect of the invention provides an apparatus for separationand selective recomposition of ions, comprising (a) a cell comprising(i) a first insulated container; (ii) a first ion selective membrane;(iii) a second ion selective membrane, wherein the first and second ionselective membranes divide the volume of the first insulated containerinto a first hydraulically isolated volume, a second hydraulicallyisolated volume and a third hydraulically isolated volume, wherein thethird hydraulically isolated volume is located between the first and thesecond hydraulically isolated volumes; (iv) a first EDLC electrodesecured within the first hydraulically isolated volume; and (v) a secondEDLC electrode secured within the second hydraulically isolated volume;and (b) an electric current supply source for connecting to andcontrolling the polarities of the first and second EDLC electrodes.

A third aspect of the invention provides an apparatus for separation andselective recomposition of ions, comprising in combination: (a) a firstcell comprising (i) a first insulated container; (ii) a first ionselective membrane; (iii) a second ion selective membrane, wherein thefirst and second ion selective membranes divide the volume of the firstinsulated container into a first hydraulically isolated volume, a secondhydraulically isolated volume and a third hydraulically isolated volume,wherein the third hydraulically isolated volume is located between thefirst and the second hydraulically isolated volumes; (iv) a first EDLCelectrode secured within the first hydraulically isolated volume; and(v) a second EDLC electrode secured within the second hydraulicallyisolated volume; (b) a second cell comprising (i) a second insulatedcontainer; (ii) a third ion selective membrane; (iii) a fourth ionselective membrane, wherein the third and fourth ion selective membranesdivide the volume of the second insulated container into a fourthhydraulically isolated volume, a fifth hydraulically isolated volume anda sixth hydraulically isolated volume wherein the sixth hydraulicallyisolated volume is located between the fourth and the fifth ones; (iv) athird EDLC electrode secured within the fourth hydraulically isolatedvolume; and (v) a fourth EDLC electrode secured within the fifthhydraulically isolated volume; (c) a first electric current supplysource for connecting to and controlling the polarities of the first andsecond electrodes; and (d) a second electric current supply source forconnecting to and controlling the polarities of the third and fourthelectrodes.

A fourth aspect of the invention provides an apparatus for separationand selective recomposition of ions, comprising in combination: (a) afirst cell comprising (i) a first insulated container; (ii) a first ionselective membrane; (iii) a second ion selective membrane, wherein thefirst and second ion selective membranes divide the volume of the firstinsulated container into a first hydraulically isolated volume, a secondhydraulically isolated volume and a third hydraulically isolated volume,wherein the third hydraulically isolated volume is located between thefirst and the second hydraulically isolated volumes; (iv) a firstelectrode secured within the first hydraulically isolated volume,wherein the first electrode is a low electrical capacitance electrodewhich allows the occurrence of electrode reactions; and (v) a secondelectrode secured within the second hydraulically isolated volume,wherein the second electrode is an EDLC electrode; (b) a second cellcomprising (i) a second insulated container; (ii) a third ion selectivemembrane; (iii) a fourth ion selective membrane, wherein the third andfourth ion selective membranes divide the volume of the second insulatedcontainer into a fourth hydraulically isolated volume, a fifthhydraulically isolated volume and a sixth hydraulically isolated volumewherein the sixth hydraulically isolated volume is located between thefourth and the fifth hydraulically isolated volumes; (iv) a half fuelcell device placed within the fourth isolated volume; and (v) a thirdelectrode secured within the fifth hydraulically isolated volume,wherein the third electrode is an EDLC electrode; (c) a first electriccurrent supply source for connecting to and controlling the polaritiesof the first and second electrodes; and (d) a second electric currentsupply source for connecting to and controlling the polarities of thethird electrode and the porous electrode of the half fuel cell structurein the fourth volume, wherein the first hydraulically isolated volumeincludes a cap, the cap including a tube connecting the empty spaceabove the first electrolyte solution to the half fuel cell device, andwherein the second current supply source includes a resistive orcapacitive load that can consume the electric energy generated betweenits two ends so that the energy is used.

A fifth aspect of the invention provides an apparatus for separation andselective recomposition of ions, comprising in combination: (a) a firstcell comprising (i) a first insulated container; (ii) a first ionselective membrane; (iii) a second ion selective membrane, wherein thefirst and second ion selective membranes divide the volume of the firstinsulated container into a first hydraulically isolated volume, a secondhydraulically isolated volume and a third hydraulically isolated volumewherein the third hydraulically isolated volume is located between thefirst and the second hydraulically isolated volumes; (iv) a firstelectrode secured within the first hydraulically isolated volume,wherein the first electrode is a low electrical capacitance electrodewhich allows the occurrence of electrode reactions; and (v) a secondelectrode secured within the second hydraulically isolated volume,wherein the second electrode is an EDLC electrode; (b) a second cellcomprising (i) a second insulated container; (ii) a third ion selectivemembrane; (iii) a fourth ion selective membrane, wherein the third andfourth ion selective membranes divide the volume of the second insulatedcontainer into a fourth hydraulically isolated volume, a fifthhydraulically isolated volume and a sixth hydraulically isolated volumewherein the sixth hydraulically isolated volume is located between thefourth and the fifth hydraulically isolated volumes; (iv) a thirdelectrode secured within the fourth hydraulically isolated volume,wherein the third electrode is a low electrical capacitance electrodewhich allows the occurrence of electrode reactions; and (v) a fourthelectrode secured within the fifth hydraulically isolated volume,wherein the fourth electrode is an EDLC electrode; (c) a first electriccurrent supply source for connecting to and controlling the polaritiesof the first and second electrodes; and (d) a second electric currentsupply source for connecting to and controlling the polarities of thethird and fourth electrodes.

The nature and advantages of the present invention will be more fullyappreciated from the following drawings, detailed description andclaims.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings illustrate embodiments of the invention and,together with a general description of the invention given above, andthe detailed description given below, serve to explain the principles ofthe invention.

FIG. 1 illustrates one embodiment of the invention including two ionrepulsion cells (IRC), two ion sinks and the command and controlinstruments according to prior art.

FIG. 2 illustrates an embodiment of the invention wherein valves areeliminated.

FIG. 3 illustrates the setup of FIG. 2 wherein the electrodes from onecell are switched with the electrodes of the other.

FIG. 4 illustrates another embodiment of the invention wherein anon-capacitive electrode is used and wherein one half cell is replacedwith a half fuel cell structure.

FIG. 5 illustrates the setup of FIG. 4 wherein the EDLC electrodes fromone half cell is switched with that of the other.

FIG. 6 illustrates another embodiment of the invention wherein each cellincludes one EDLC and one non-capacitive electrode.

FIG. 7 illustrates the setup of FIG. 6 wherein the EDLC electrodes fromone half cell is switched with that of the other.

DETAILED DESCRIPTION OF THE INVENTION

As noted above, the scientific foundations of the present invention havebeen detailed in U.S. Pat. Nos. 8,715,477, 9,309,133 and 9,315,398 tocurrent inventor A. Yazdanbod, which teach a number of embodiments ofIon Separation and Recomposition Technology (ISART). Generally, thesepatents teach that oppositely charged ions can be separately extractedfrom two differing input solutions, resulting in depletion of ions fromthe input solution and generation of two ionic streams, i.e. a positiveionic stream and a negative ionic stream, each having an excess of onepolarity of ions. The oppositely charged ionic streams from each of thetwo differing solution can then be drawn into an ion sink and combinedto form different, new solutions or chemical compounds as compared withthe original input solutions.

Briefly, when two single Electric Double Layer Capacitor (EDLC)electrodes (i.e. a capacitive electrode which functions in a capacitivemode without the occurrence of electrode reactions) are each placedinside a separate electrolyte filled insulated container, herein calledIon Repulsion Cells (IRCs), and a DC voltage is applied between thesetwo electrodes, there will be an excess of ions (having the samepolarity as the charge applied to the electrode) that will concentrateat the outer edge of each of the individual containers. EDLC electrodesare made of electrically conductive material, such as carbon aerogels,carbon aerogel composites or any electrically conductive materialexhibiting such electric capacitances of more than 1 Farads per gram,preferably more than 10 Farads per gram, and ideally more than 50 Faradsper gram. When placed in contact with an electrolyte solution and DCvoltage is applied, EDLC electrodes absorb ions and create an electricdouble layer of ions on the electrode. If the IRCs are hydraulicallyconnected by a tube to a third container, herein called an Ion Sink, andthere is an Ion Selective Membrane (ISM) associated with each of thesetubes which create an ion selective barrier within the interiorcross-section of these tubes, and if the polarity of each ISM is suchthat it would prevent the flow of ions of opposite polarity and allowions of the same polarity of the ions accumulated on the inner surfaceof the related IRC, then there will be an ionic current of singlepolarity generated from each IRC, each having opposite polarity ionswith respect to the other, entering the Ion Sink and neutralizing theother in the Ion Sink.

FIG. 1 illustrates a classic prior art embodiment of Ion Separation andRecomposition Technology (ISART). This typical embodiment includes twoIon Repulsion Cells (IRCs), two ion sinks, four control valves, four ionexchange membranes and command and control instruments. Looking at FIG.1, a first IRC 1 includes a first insulated container 2 made fromnonconductive material, containing a first electrolyte solution 3 filledto a level 4, and a first EDLC electrode 5. There is also a second IRC21 having identical elements as the first IRC 1, namely a secondinsulated container 22 made from nonconductive material, containing asecond electrolyte solution 23 filled to a level 24, and a second EDLCelectrode 25. A first pair of flexible tubes or pipes 6 and 7 areconnected to the first IRC 1, and an identical second pair 26, 27 areconnected to the second IRC 21. Each of the pipes 6, 7, 26, 27 areequipped with inline filter holders 8, 9, 28, 29, respectively, eachfilter holder containing ion exchange membranes of a single polarity,herein referred to as Ion Selective Membranes or ISMs. Pipes 6 and 26include first and second flow cut-off valves 31 and 32, respectively,and pipes 7 and 27 include third and fourth flow cut-off valves 33 and34, respectively. IRCs 1 and 21 are hydraulically connected to a firstion sink 41 through pipes 6 and 26 and to a second ion sink 51 throughpipes 7 and 27. Ion sink 41 includes a third insulated container 42,made from nonconductive material, filled with electrolyte 43 to level44. Ion sink 51 includes a third insulated container 52, made fromnonconductive material, filled with electrolyte 53 to level 54.

A direct current electric current supply source 60 capable of polarityreversal and having electric ports 61 and 62 is included. Each of thefirst and second EDLC electrodes 5 and 25 are connected to a metallicwire, 70 and 71 leading out of the IRC and connected to one pole of thepower supply 60 through wires 74 and 75 respectively. Electric ports 61and 62 could each be either positive or negative polarity. Power supply60 also has another port 66 that outputs a given electric signal thatchanges depending on the polarity between poles 61 and 62. Cable 79connects this port 66 to port 81 of a control device 80. The four outputports, shown together as outlet 82 of the control device 80, are eachconnected through appropriate cables (not shown) to one of the flowcut-off valves 31, 32, 33, 34. The control device 80 senses the polaritydependent signal through port 66 and switches the first and second flowcut-off valves 31 and 32 to a first orientation, e.g. to an openposition, while simultaneously switching the third and fourth flowcut-off valves 33 and 34 to the opposite orientation, e.g. to a closedposition.

For example, when the system is operated, the first EDLC electrode 5could be negatively charged while the second EDLC electrode 25 could bepositively charged. If, under this condition, flow cut-off valves 31 and32 are open, and valves 33 and 34 are closed through the action of thecontrol device 80, the ion selective membranes in inline filter holders8 and 29 will be anion exchange membranes while the membranes in thefilter holders 9 and 28 will be cation exchange membranes. Withreference now to FIG. 1, it can be appreciated that if the power supply60 is energized to any DC voltage level such that pole 62 is at a higherpotential than pole 61 as stated before (and assuming that theelectrical insulation capabilities of the insulated containers 2 and 22are sufficient to prevent exchange of electric charge between thecontainer and the outside environment), the build-up of potentialbetween electrodes 5 and 25 will lead to generation of single oppositelycharged ion currents flowing out of the two IRCs and into Ion Sink 41,neutralizing each other therein. This means that anions will now flowout of IRC 1 and cations will flow out of IRC 21 and the two willneutralize one another in the Ion Sink 41. At the same time, thecapacitance of each EDLC electrode 5 and 25 will begin to fill.

Under this condition, if the first electrolyte solution 3 in IRC 1 is asolution of silver nitrate (AgNO₃) and the second electrolyte solution23 in IRC 21 is a solution of sodium chloride (NaCl), silver ions (Ag⁺)will begin to be capacitively absorbed to electrode 5 and chlorine ions(Cl⁻) will begin to be capacitively absorbed to electrode 25. At thesame time, an ionic current of nitrate ions (NO₃ ⁻) will pass throughtube 6 and inline filter 8 (containing an ion selective membrane ISM),entering Ion Sink 41 while an ionic current of sodium (Na⁺) will flowout of IRC 21 through line 26 and ISM 28 and will also enter Ion Sink41, neutralizing the nitrate ion stream and together forming a sodiumnitrate solution (NaNO₃) in Ion Sink 41. Once the potential between oneor both electrodes 5 and 25 and the ions capacitively absorbed to eachelectrode reach a level that would allow electrode reactions to occurbetween the ions and the electrode they are capacitively absorbed to,that is, once one or both these capacitors fill up, the polarity of theelectric current supplied by power supply 60 could be reversed,signalling the control device 80 to close valves 31 and 32, and openvalves 33 and 34. This reversal of applied potential to electrodes 5 and25 will initially release the ions previously absorbed to theseelectrodes and in continuation of the process, will result in absorptionof charges of opposite polarity with respect to the previously absorbedions on the electrodes. This reversal of polarity combined with closureof valves 31 and 32 and the opening of valves 33 and 34 will nowgenerate two oppositely charged ionic currents into Ion Sink 51. Thus,IRC 1 will now generate a sliver ion (Ag⁺) current while IRC 21 will nowgenerate a chlorine ion (Cl⁻) current. These ionic currents pass throughpipes 7 and 27, as well as ISM 9 and ISM 29, and neutralize each otherin Ion Sink 51, forming silver chloride (AgCl) which precipitatestherein. This was experimentally verified as reported in U.S. Pat. Nos.8,715,477, 9,309,133 and 9,315,398. Once the capacitances of theelectrodes fill up with ions or at any other earlier convenient time,the polarity of the voltage applied by power supply 60 is reversed againand the process switches to the formation of sodium nitrate (NaNO₃) inIon sink 41 and then again to formation of silver chloride (AgCl) in IonSink 51 and so on.

There are other embodiments of Ion Separation and RecompositionTechnology, as illustrated in U.S. Pat. Nos. 8,715,477, 9,309,133 and9,315,398 (e.g. FIG. 3), wherein one IRC is equipped with an EDLCelectrode while the other has a non-capacitive, typically metallic orcarbon electrode. In this setup, the IRC with the non-capacitiveelectrode is used, for example, to generate hydroxide (OH⁻) ions towardsthe related Ion Sink; here, the generated hydrogen gas exiting thesolution is ionized in a half fuel cell structure and is reacted withthe negatively charged ions generated by the first IRC in the secondphase of operation to produce such compounds as hydrochloric acid. Thereis also the embodiment wherein there is one capacitive IRC and twonon-capacitive IRCs, as illustrated in U.S. Pat. Nos. 8,715,477,9,309,133 and 9,315,398 (e.g. FIG. 4). While certainly useful aspatented, it is notable that all of the embodiments presented in theseISART patents include valves (e.g. 31-34) that close the path ofcommunication to one Ion Sink while the other Ion Sink is being used,such that half of the time one of the Ion Sinks sits idle.

For example, in each half cycle operation of a given ion repulsion cell,one of the two valves each placed on the passage leading to an ionexchange membrane and its related ion sink is closed and the other isopened. This means that half of the time, one ion exchange membrane setand their related ion sink are used while the other ion exchangemembrane set and its related ion sink sit idle. Thus, productioncapacity is technically reduced by 50% compared to full utilization ofeach ion exchange membrane and each cell. Further, in each half cycle ofoperation, a given valve needs to initially close and then re-open inthe next half cycle. This places a lot of stress on the system andrequires a good deal of maintenance work to insure that these largesurface area valves remain electrically and hydraulically sealed whenclosed.

It would therefore be advantageous for certain industrial applicationsof the ISART technology if one were to eliminate the need for valves tooperate the ion repulsion cells and to be able to continuously operateeach ion sink. Indeed, if these valves could be eliminated, theconnection passages between the ion sinks and ion repulsion cells can bemade shorter, the surface areas of the ion exchange membranes can beincreased, and each ion exchange membrane set and its related ion sinkcan be utilized almost continuously. The present invention results fromthe discovery that, by eliminating the flow cut-off valves 31, 32, 33,34 (see FIG. 1) and moving the ion filled electrodes, the output of theISART system discussed above can be nearly doubled.

FIG. 2 presents such an alternative apparatus 200 for ISART, accordingto the present invention. In this apparatus, there are first and secondinsulated containers 101, 201 also referred to as Cells, which aretypically cuboid in shape, but may be in any suitable shape. Cell 101includes first and second Ion Selective Membranes (ISMs) 108, 128, andCell 201 includes third and fourth ISMs 208 and 228. In Cell 101, ISM108 is an anion exchange membrane and ISM 128 is a cation exchangemembrane. In Cell 201, ISM 208 is a cation exchange membrane andmembrane 228 is an anion exchange membrane. These membranes (108, 128,208, 228) are completely sealed against the inner surface of theirrespective containers and divide the volume of each cell (101, 201) intothree hydraulically isolated sections. Specifically, the resultingvolumes in container 101 include first, second and third hydraulicallyisolated volumes or sections 103, 123 and 141, respectively, andlikewise container 201 is divided into fourth, fifth and sixthhydraulically isolated sections 203, 223 and 241, respectively. Here,hydraulic isolation means that the liquid in each section is separatedfrom the liquid in the adjacent sections as the ISMs are basicallyimpervious to liquids and are perfectly sealed against the inner wall ofthe container they are in. Cell 101 also includes a first highcapacitance EDLC electrode 105 in the first hydraulically isolatedvolume 103, and a second EDLC electrode 125 in the second hydraulicallyisolated volume 123. Similarly, cell 201 includes a third EDLC electrode205 and a fourth EDLC electrode 225 in hydraulically isolated volumes203 and 223, respectively. A direct current electric power source 160includes pole 161 connected to electrode 105 via wire 174, and pole 162connected to electrode 125 via wire 175. Similarly, a DC electric powersupply 260 includes pole 261 connected to electrode 205 via wire 274,and pole 262 connected to electrode 225 via wire 275.

As shown FIG. 2, the three ISM-divided sections in each of cells 101 and201 are each filled with an electrolyte solution to levels 104, 124 and126 in cell 101 and to levels 204, 224 and 226 in cell 201. When thepower supply 160 is turned on for cell 101, with pole 161 being negativeand pole 162 being positive as shown, the interaction of the first EDLCelectrode 105 with the electrolyte solution in section 103 will resultin absorption of positively charged ions in the electrolyte solution toelectrode 105, and repulsion of negatively charged ions towards theouter perimeter of the volume within section 103, which is the innersurface of section 103, including ISM 108. Similarly, in section 123there will be negatively charged ions from the electrolyte solutionabsorbed to electrode 125, with positive ions being repulsed towards theouter perimeter of the volume within section 123, including ISM 128.With ISM 108 being an anion exchange membrane and ISM 128 being a cationexchange membrane, the repulsed ions from sections 103 and 123 passthrough their respective ISM and enter middle section 141, where theycan form a new compound combining the negative ions passing from section103 and the positive ions passing from section 123. Meanwhile, withabsorption of ions onto EDLC electrodes 105 and 125, the electric doublelayer capacitor formed between these ions and charges on the conductivebody of each electrode begins to fill up, creating a potentialdifference between the two plates of the each EDLC electrode.

When the power supply 260 is turned on for cell 201 while cell 101 isbeing operated, the same series of phenomena occurring in cell 101 willoccur in cell 201, but with opposite charges. Specifically, with pole261 being positively charged and pole 262 being negatively charged,negative ions in the solution in section 203 will be absorbed toelectrode 205 and positive ions will be repulsed towards the outerperimeter of section 203 (i.e. towards the inner surface of section 203,including ISM 208). Further, in section 223 there will be absorption ofpositive ions onto electrode 225 and repulsion of negative ions to theouter perimeter of section 223. With ISM 208 being a cation exchangemembrane and ISM 228 being an anion exchange membrane, the repulsed ionsfrom sections 203 and 223 pass through their respective ISM and entermiddle section 241, where they can form a new compound combining thepositive ions passing from section 203 and the negative ions passingfrom section 223. Meanwhile, with absorption of ions onto EDLCelectrodes 105 and 125, the capacitor formed between these ions andcharges on the conductive body of each electrode begins to fill up,creating a potential difference between the two plates of the each EDLCelectrode.

Now, if the electrolyte solutions in sections 103 and 203 are the same,such as a solution of silver nitrite (AgNO₃), and if the electrolytes insections 123 and 223 are also the same, such as a solution of sodiumchloride (NaCl), positive silver ions (Ag⁺) will be absorbed toelectrode 105 and negative chlorine ions (Cl⁻) will be absorbed toelectrode 125. Thus, negative nitrate ions (NO₃ ⁻) will be repulsed fromsection 103 and pass through ISM 108 (which is an anion exchangemembrane) to enter the middle section 141 (i.e. the third hydraulicallyisolated volume 141 of cell 101), where they can encounter andneutralize positive sodium (Na⁺) ions being repulsed from volume 123 andpassing through ISM 128 (which is an cation exchange membrane), formingsodium nitrate (NaNO₃). Similarly, but with the charges on theelectrodes being the reverse of those of electrodes 105 and 125, theions absorbed to electrode 205 in cell 201 will be nitrate ions (NO3⁻)and the ions absorbed to electrode 225 will be sodium ions (Na⁺). Thus,positive silver ions (Ag⁺) will be repulsed from section 203 and passthrough ISM 208 (which is an cation exchange membrane) to enter middlesection 241 (i.e. the sixth hydraulically isolated volume 241 of cell201), where they can encounter and neutralize negative chlorine ions(Cl⁻) being repulsed from section 223 and passing through ISM 228 (whichis an anion exchange membrane), forming silver chloride (AgCl) as aprecipitate.

Comparing FIG. 1 to FIG. 2, it can be appreciated that, while no valvesare present, the first, second, fourth and fifth hydraulically isolatedvolumes/sections 103, 123, 203 and 223 all function as Ion RepulsionCells (IRCs) and the third and sixth hydraulically isolated sections 141and 241 function as Ion Sinks, as described above.

As noted above, ions of opposite polarity are capacitively absorbed toeach EDLC electrode, creating a potential difference between theelectrode and the surrounding electrolyte solution (due to the flow ofions out of each IRC). Once this potential difference reaches the levelwherein electrode reactions (i.e. redox reactions) begin to occurbetween the absorbed ions and the electrodes, then the electrodes aresaturated with ions and can no longer store additional ions. Morespecifically, with continuous operation of this system and theconsequent further increase of the number of ions capacitively absorbedto each electrode, redox reactions occur such that absorbed positiveions on electrodes gain electrons from the negatively charged electrodes(such as Ag⁺ ions gaining an electron and becoming elemental silver) andthe absorbed negative ions on positively charged electrodes giveelectrons to the electrodes (such as Cl⁻ ions giving an electron to theelectrode and becoming chlorine gas).

FIG. 3 shows the embodiment of FIG. 2, except that the EDLC electrodesfrom cells 101 and 201 have been switched to avoid redox reactions atthe EDLC electrodes. That is, when redox reactions begin to occur or atany other convenient time before this point, EDLC electrodes 105 and 205from FIG. 2 can be switched between sections 103 and 203, respectively,and EDLC electrodes 125 and 225 can also be switched between sections123 and 223, respectively. That is, as shown in FIG. 3, electrode 105 isplaced in section 203 of cell 201, and electrode 205 is placed insection 103 of cell 101, while electrode 125 is placed in section 223,and electrode 225 is placed in section 123. With this embodiment, whenthe power supply units 160, 260 are turned on, the previously storedions on each EDLC electrode will begin being repulsed from theelectrode, entering the surrounding solution. Further, these electrodeswill now also begin to absorb ions of opposite polarity compared to theones being removed from them.

For example, looking at FIG. 3, electrode 205 that is now connected topole 161 and is receiving electrons (−) from the power supply will beginrepulsing the previously absorbed nitrate ions (NO3⁻) and will beginabsorbing silver ions (Ag⁺) from the adjacent silver nitrate solution.The newly released nitrate ions will then move to the outer perimeter ofsection 103, as before, and move through the respective ISM 108 andenter the associated ion sink 141, while the previously stored sodiumions are repulsed from the positive EDLC electrode 225, which now beginsto absorb chloride ions, such that positive sodium ions passing throughISM 128 join with the negative nitrate ions in ion sink 141 to createsodium nitrate (NaNO₃). This process will also occur for the silver ionspreviously absorbed to EDLC electrode 105 and those additional silverions repulsed from the silver nitrate electrolyte solution in IRC 203,and for chlorine ions stored on electrode 125 and those additionalchlorine ions repulsed from the sodium chloride electrolyte solution inIRC 223, such that silver and chloride ion streams will now pass throughISM 208 and ISM 228 respectively and will enter ion sink 241 to producesilver chloride. This process can be run continuously, except for theperiod of time it takes to switch the EDLC electrodes from one IRC tothe other. Once again, when the capacitors at EDLC electrodes approachtheir capacity or at any earlier convenient time, the switching of thelocation of electrodes can be repeated as before, ensuring almostcontinuous production of the products in both ion sinks 141, 241.

Another embodiment of the present invention is shown in FIG. 4, which isdesigned to resolve the underutilization of prior art ISART cells wherewater (H₂O) is one of the electrolyte solutions, and also addresses theproduction of acids or basis where hydrogen and hydroxide ions areneeded. In FIG. 4 all components are the same as in FIG. 2, except forthe following: (1) the EDLC electrode 105 in FIG. 2 is replaced by lowcapacitance electrode 305; (2) hydraulically isolated section 203 ofFIG. 2 (including EDLC electrode 205 and the electrolyte solution, sinceall collectively serves as an Ion Repulsion Cell) is replaced in FIG. 4by a half fuel cell device 191, which will be described in more detailbelow; (3) section 103 is now capped, and there is a tube 190 connectingthe empty space above the electrolyte solution level 104 to half fuelcell device 191; and (4) power supply unit 260 now includes an electricload 306, through which poles 261 and 262 of DC power supply 260 can beconnected to one another when the power supply is turned off. Electricload 306 can be an electric circuit (or any combination of electriccircuits) that can consume the electric energy generated between its twoends, such as a resistive load or capacitive load, so that the energy isused.

Regarding the low capacitance electrode 305 in FIG. 4, while the firstEDLC electrode 105 (as well as electrodes 125, 205 and 225) of FIG. 2are typically made of an electrically conductive material such as carbonaerogel having an electric capacitance from about 1 Farad per gram tomore than 50 Farads per gram, the low capacitance electrode 305 istypically a metallic or simple carbon electrode. Such metallic or simplecarbon electrodes typically have capacitances in the order of severalmicro-micro Farads (μμF or 1*10⁻¹² Farads) In the embodiment shown inFIG. 4, the electrolyte solution in section 103 is a solution of aspecifically selected compound targeted to production of H⁺ or OH⁻ ions,and the electrolyte solution in section 123 is a high concentrationsolution of the raw material such as sodium chloride. Using thisconfiguration, and when the goal is for IRC 103 to generate OH ions, theelectrolyte solution in IRC 103 must contain cations that have lowerelectrode potential than H⁺ ions, such as sodium or lithium.

Thus, when an electrolyte solution such as sodium hydroxide (NaOH,caustic soda) is placed in section 103, and with low capacitanceelectrode 305 being connected to a cathode pole, OH⁻ ions will passthrough ion exchange membrane (ISM) 108 and stream out of section 103into ion sink 141, while redox reactions at the low capacitanceelectrode 305 cause hydrogen gas (H₂) to emit from IRC 103 to the emptyspace above it. Inversely, when the goal is for IRC 103 to generate H+ions, the electrolyte solution in section 103 should contain anions thathave higher electrode potential than OH⁻, such as sulfuric acid (H₂SO₄).Under these conditions, the low capacitance electrode 305 will be ananode, redox reactions at electrode 305 will cause oxygen gas (O₂) to beemitted from IRC 103 to the empty space above it, and a stream of H⁺ions will pass through ISM 108 and into ion sink 141.

More specifically, looking at FIG. 4, when the electrolyte solution inhydraulically isolated section 103 is a solution of caustic soda (NaOH),the low capacitance electrode 305 is negatively charged, ISM 108 is ananion exchange membrane allowing the passage of negative ions, and ISM128 is a cation exchange membrane allowing the passage of positivelycharged ions, the operation of the DC power source 160 will result inconnection of a negative potential to the metallic electrode 305 andpositive potential to the EDLC electrode 125. With sufficient electricpotential applied, electrode reactions (Redox reactions) are initiatedat electrode 305, which is bathed in NaOH solution. The electrolytesolution in the hydraulically isolated section 123 as well as theelectrolyte in section 223 would typically be sodium chloride. Repulsionof positively charged sodium ions from section 123 will occur due tocapacitive absorption of chlorine ions to the high capacitance EDLCelectrode 125. Under these conditions, there will be a stream of OH⁻ions from IRC 103 and the repulsion of a stream of sodium ions from IRC123, with both streams entering ion sink 141 and leading to theformation of caustic soda (NaOH) in ion sink 141. The use of causticsoda as electrolyte solution in IRC 103 will also result in generationof hydrogen gas (H₂) at the metallic electrode 305, which enters theempty space above level 104.

It should be noted that if the requirements of a particular design donot require the separation of the electrolyte solutions in section 103and ion sink 141, then the corresponding ISM 108 can also be eliminated.Thus, in the example above, since NaOH is present in both section 103and ion sink 141, ISM 108 could be eliminated. The reverse is true aswell, that is, if by necessities of a design such as differences inconcentration or compositions the electrolytes in volumes 103 and 141need to be kept separate, ISM 108 will have to be used. Furthermore,given the very high pH of the caustic soda electrolyte used in volume103 in the example above, and the subsequent formation of high pHcaustic soda in volume 141, both ISM 108 (if needed) and ISM 128 wouldhave to be of material that are stable in high pH environments.

FIG. 5 illustrates switching of EDLC electrodes 125 and 225, similarlyas described above and shown in FIG. 3. Specifically, when thecapacitors at EDLC electrodes 125 and 225 approach their capacity suchthat Redox reactions begin to occur (or at any earlier convenient time),the switching of the location of these electrodes can be done, ensuringalmost continuous production of the desired product. Specifically,electrode 125 can be removed from volume 123 and then be placed involume 223, while electrode 225 can be removed from section 223 andplaced in section 123. This will allow electrode 225 to function involume 123 in the same manner as electrode 125 functioned when it was involume 123.

With DC power source 260 including electric load 306 connecting poles261 and 262, moving EDLC electrode 125 (now containing a certain amountof chlorine ions) to volume 223 of cell 201 can cause electrode 125 toreceive electrons generated by half fuel cell device 191. This can causeEDLC electrode 125 to release its chlorine ion (Cl⁻) content and allowinteractions with hydrogen ions (H⁺) produced by device 191. Looking atFIG. 5, device 191 is a half fuel cell structure made up of an entryvolume 307, a porous conductive electrode 308 made up of material suchas carbon cloth, and an ISM 208 that in this case would have to bestable in the very low pH, acidic solutions produced in ion sink 241. Tobe able to ionize the hydrogen gas, the porous conductive electrode 308should be coated with catalysts such as platinum or platinum black.Platinum black is widely used as a thin film on carbon cloth in fuelcells or for covering solid platinum metal, forming platinum electrodes.This “platinized platinum” has a surface area much higher than thegeometrical surface area of the electrode, and exhibits action superiorto that of platinum.

Hydrogen gas (H₂) entering from tube or conduit 190 can be ionized bydevice 191, splitting into an electron and a proton, wherein a stream ofpositively charged hydrogen ions (H⁺, protons) can pass through the ISM208 and combine with the negatively charged chlorine ions released fromelectrode 125 to form hydrochloric acid (HCl) in ion sink 241. At thesame time, the negative electrons produced by ionization of the hydrogengas will go through the electric load 306 of the DC power source 260 andback to electrode 125, making electrode 125 a cathode and facilitatingthe removal of chlorine ions therefrom. The potential difference acrossthe electric load 306 is caused by the potential difference between theporous electrode 308 and electrode 125. This potential difference andthe charges energized by it could then do work across the electric load306. Alternatively, and with attention to FIG. 5, the electric load 306could be eliminated and the DC power source 260 could be turned on toaccelerate the formation of hydrochloric acid in ion sink 241 whilenegatively charging the EDLC electrode 125, causing IRC 223 to generatemore chlorine ions and absorbing sodium ions to the EDLC electrode 125.After this operation, the now sodium ion-loaded electrode 125 can bereturned to IRC 123, and electrode 225 that is now loaded with chlorineions can be returned to IRC 223, so that the production of caustic soda(NaOH) in ion sink 141 and hydrochloric acid (HCl) in ion sink 241 canproceed continuously (except for the time it takes to switch theelectrodes).

An alternative embodiment of the present invention is illustrated inFIG. 6 and FIG. 7. In FIG. 6 all components are the same as in FIG. 2,with the exception that the two high capacitance EDLC electrodes 105 and205 have been replaced with low capacitance metallic or carbonelectrodes 305 and 405, respectively. This system is capable ofbenefiting from Redox reactions occurring in both hydraulically isolatedsections 103 and 203, such that both acids and bases can be produced.With this arrangement a base solution can be caused to form in ion sink141. Specifically, low capacitance, metallic electrode 305 can be placedin volume 103 containing an electrolyte solution of caustic soda (NaOH).With an applied potential from power source 160, section 103 acts as anIRC to generate a stream of hydroxide ions (OH⁻) passing through ISM 108to enter ion sink 141. Hydrogen gas (H₂) will be emitted above level 104due to Redox reactions taking place at electrode 305. Now, if theelectrolyte solution in hydraulically isolated volume 123 is a solutionof ammonium chloride (NH₄Cl), EDLC electrode 125 will cause therepulsion of positively charged ions through cation exchange membrane(ISM) 128, such that section 123 acts as an Ion Repulsion Cell (IRC) togenerate a stream of ammonium ions (NH4⁺) passing through ISM 128 toenter ion sink 141. With this arrangement, the hydroxide (OH⁻) ionstream from volume 103 and the ammonium (NH4⁺) ion stream from volume123 can combine in ion sink 141 to form a solution of ammonium water(typically denoted by the formula NH₄OH).

Simultaneously, low capacitance electrode 405 (acting as an anode) canbe can be placed in volume 203 containing an electrolyte solution ofsulfuric acid (H₂SO₄), and EDLC electrode 225 (acting as a cathode) canbe placed in volume 223 containing an electrolyte solution of ammoniumchloride (NH₄Cl). With an applied potential provided by power source260, section 203 acts as an IRC to generate a stream of hydrogen ions(H⁺) that pass through cation exchange membrane ISM 208 to enter ionsink 241, while redox reactions take place at electrode 405, emittingoxygen (O₂) gas out above level 204. Section 223 will act as an IonRepulsion Cell (IRC) to generate a stream of chlorine ions (Cl⁻) passingthrough ISM 228 to enter ion sink 241, such that the hydrogen andchloride ion streams can combine in ion sink 241 to form hydrochloricacid (HCl). This has been experimentally verified by the presentinventor.

FIG. 7 illustrates switching of EDLC electrodes 125 and 225, similarlyas described above and shown in FIGS. 3 and 5. Specifically, when thecapacitors at EDLC electrodes 125 and 225 approach their capacity suchthat Redox reactions begin to occur (or at any earlier convenient time),the switching of the location of these electrodes can be done, ensuringalmost continuous production of the desired product. Specifically,chlorine ion-containing EDLC electrode 125 can be removed from volume123 and placed in volume 223, while ammonium ion-containing EDLCelectrode 225 can be removed from section 223 and placed in section 123.This will allow production of ammonium hydroxide (NH₄OH) in ion sink 141and hydrochloric acid (HCl) in ion sink 241 to continue uninterrupted,but for the time required to switch the location of electrodes 125 and225.

In verification experiments carried out on this process using a cellclosely adhering to cell 101 in FIG. 6, i.e. with hydraulically isolatedvolume 103 containing caustic soda (NaOH) and volume 123 containingammonium chloride (NH₄Cl), thereby sending ammonium and hydroxide ionstreams to ion sink 141, it was observed that due to the rather lowsolubility of ammonia in water at room temperature (about 18 mole perliter), evaporation of ammonia from the surface of ion sink 141 couldeasily be observed by its distinct smell and by the use of a wet pHdetection paper that turned dark blue (signifying high pH in the rangeof 13 to 14), signifying emergence of ammonia from the solution formedtherein.

The various embodiments of the present improvement of the ISART processdescribed herein can be applied to the industrial production of SodaAsh. As noted above, the Solvay Process is one of the main industrialprocesses currently used for manufacturing sodium carbonate (i.e. SodaAsh), but the process involves many intermediate steps and producesnon-useful by-products. To solve these problems, the present inventorsurmised that the ISART process could be a likely candidate to improvethe production process of Soda Ash. However, due to low solubility ofsome of the input compounds, ISART production of soda ash was found toproceed at a slow rate. For example, using the presently used rawmaterials used in the Solvay Process, namely limestone (calciumcarbonate), salt brine (sodium chloride) and ammonia, it was believedthat ISART could be used to easily and efficiently form sodium carbonateby replacing the calcium ions in calcium carbonate with sodium ions fromsodium chloride; and the process would also be useful to combine theremaining oppositely charged ions, namely chlorine and calcium ions, tofrom calcium chloride. While in theory all looked good, it was foundthat the low solubility of limestone/calcium carbonate slows down theISART process to a point of impracticality. Although the solubility ofcalcium carbonate in water can be increased by pressurizing the solvent(i.e. water) with carbon dioxide and dissolving it in the water, theimproved solubility was determined to be insufficient for largeindustrial applications. The low solubility of calcium carbonate thusplaces a limitation on the capability of ISART for the industrialproduction of sodium carbonate using the raw materials of the SolvayProcess.

To overcome such limitations, the present inventor has improved theISART process so that it is practical to produce industrial amounts ofsoda ash. Thus it is possible to change the Solvay process to onesimilar to Hou's process, by using carbon dioxide (CO₂) as an inputwhile at the same time producing hydrochloric acid and recoveringammonia for reuse, without any need for lime. Here, referring to FIGS.4, 5, 6 and 7 and the process described earlier for production ofcaustic soda and hydrochloric acid, it could be appreciated that ifsimultaneous with production of caustic soda in Ion Sink 141 carbondioxide is injected into this Ion Sink, the resulting product will becaustic soda according to the following equation:

2NaOH+CO₂→Na₂CO₃+H₂O   (Equation 7)

Therefore, the ISART process can produce Soda Ash more easily if CO₂ gasis introduced as one of the input materials eliminating the need forammonia. Yet another variation would be to use carbon dioxide in asimilar column as in Solvay process where instead of producing carbondioxide by calcining lime stone, another source of carbon dioxide isused for injecting into the solution comprising a mixture of ammonia andsodium chloride as in Equation 3 and processing the remaining solutionof ammonium chloride using ISART to recover the ammonia as describedwith respect to FIGS. 6 and 7. Here in place of practically uselesscalcium chloride, hydrochloric acid will be produced. This eliminatesthe need for continuous supply of ammonia as well.

While the present invention has been illustrated by the description ofembodiments and examples thereof, it is not intended to restrict or inany way limit the scope of the appended claims to such detail.Additional advantages and modifications will be readily apparent tothose skilled in the art. Accordingly, departures may be made from suchdetails without departing from the scope of the invention.

What is claimed is:
 1. An apparatus for separation and selectiverecomposition of ions, comprising in combination: a) a first cellcomprising: i) a first insulated container; ii) a first ion selectivemembrane; iii) a second ion selective membrane, wherein the first andsecond ion selective membranes divide the volume of the first insulatedcontainer into a first hydraulically isolated section, a secondhydraulically isolated section and a third hydraulically isolatedsection, wherein the third hydraulically isolated section is locatedbetween the first and the second ion selective membranes, and whereinthe third hydraulically isolated section serves as a first ion sinkallowing for the formation of new chemical compounds; iv) a firstelectrode secured within the first hydraulically isolated section; andv) a second electrode secured within the second hydraulically isolatedsection; b) a second cell comprising: i) a second insulated container;ii) a third ion selective membrane; iii) a fourth ion selectivemembrane, wherein the third and fourth ion selective membranes dividethe volume of the second insulated container into a fourth hydraulicallyisolated section, a fifth hydraulically isolated section and a sixthhydraulically isolated section, wherein the sixth hydraulically isolatedsection is located between the third and the fourth ion selectivemembranes, and wherein the sixth hydraulically isolated section servesas a second ion sink allowing for the formation of new chemicalcompounds; iv) a third electrode secured within the fourth hydraulicallyisolated section; and v) a fourth electrode secured within the fifthhydraulically isolated section; c) a first electric current supplysource for applying an electric potential difference between the firstelectrode and the second electrode; and d) a second electric currentsupply source for applying an electric potential difference between thethird electrode and the fourth electrode.
 2. The apparatus of claim 1,wherein the first ion selective membrane is an anion selective membrane,the second ion selective membrane is a cation selective membrane, thethird ion selective membrane is a cation selective membrane, and thefourth ion selective membrane is an anion selective membrane.
 3. Theapparatus of claim 1, wherein the first electrode is an EDLC electrode,the second electrode is an EDLC electrode, the third electrode is anEDLC electrode, and the fourth electrode is an EDLC electrode.
 4. Theapparatus of claim 3, wherein each of the ion selective membranes allowsthe passage of ions of the same polarity as the charge applied to theEDLC electrode in its related hydraulically isolated section.
 5. Theapparatus of claim 3, wherein during use the first electrode is removedfrom the first electrolyte solution and placed in the third electrolytesolution, the third electrode is removed from the third electrolytesolution and placed in the first electrolyte solution, the secondelectrode is removed from the second electrolyte solution and placed inthe fourth electrolyte solution, and the fourth electrode is removedfrom the fourth electrolyte solution and placed in the secondelectrolyte solution, before occurrence of redox reactions at the EDLCelectrodes.
 6. An apparatus for separation and selective recompositionof ions, comprising in combination: a) a first cell comprising: i) afirst insulated container; ii) a first ion selective membrane; iii) asecond ion selective membrane, wherein the first and second ionselective membranes divide the volume of the first insulated containerinto a first hydraulically isolated section, a second hydraulicallyisolated section and a third hydraulically isolated section, wherein thethird hydraulically isolated section is located between the first andthe second ion selective membranes, and wherein the third hydraulicallyisolated section serves as a first ion sink allowing for the formationof new chemical compounds; iv) a first EDLC electrode secured within thefirst hydraulically isolated section; and v) a second EDLC electrodesecured within the second hydraulically isolated section; b) a secondcell comprising: i) a second insulated container; ii) a third ionselective membrane; iii) a fourth ion selective membrane, wherein thethird and fourth ion selective membranes divide the volume of the secondinsulated container into a fourth hydraulically isolated section, afifth hydraulically isolated section and a sixth hydraulically isolatedsection, wherein the sixth hydraulically isolated section is locatedbetween the third and the fourth ion selective membranes, and whereinthe sixth hydraulically isolated section serves as a second ion sinkallowing for the formation of new chemical compounds; iv) a third EDLCelectrode secured within the fourth hydraulically isolated section; andv) a fourth EDLC electrode secured within the fifth hydraulicallyisolated section; c) a first electric current supply source for applyingan electric potential difference between the first EDLC electrode andthe second EDLC electrode; and d) a second electric current supplysource for applying an electric potential difference between the thirdEDLC electrode and the fourth EDLC electrode, wherein the polarity ofcharges applied to the first EDLC electrode and the fourth EDLCelectrode are the same and the polarity of the charges applied to thesecond EDLC electrode and the third EDLC electrode are the same.
 7. Theapparatus of claim 6, wherein the first ion selective membrane is ananion selective membrane, the second ion selective membrane is a cationselective membrane, the third ion selective membrane is a cationselective membrane, and the fourth ion selective membrane is an anionselective membrane.
 8. The apparatus of claim 6, wherein each of the ionselective membranes allows the passage of ions of the same polarity asthe charge applied to the electrode in its related hydraulicallyisolated section.
 9. The apparatus of claim 6, wherein during use thefirst EDLC electrode is removed from the first electrolyte solution andplaced in the third electrolyte solution, the third EDLC electrode isremoved from the third electrolyte solution and placed in the firstelectrolyte solution, the second EDLC electrode is removed from thesecond electrolyte solution and placed in the fourth electrolytesolution, and the fourth EDLC electrode is removed from the fourthelectrolyte solution and placed in the second electrolyte solution,before occurrence of redox reactions at the EDLC electrodes.
 10. Anapparatus for separation and selective recomposition of ions, comprisingin combination: a) a first cell comprising: i) a first insulatedcontainer; ii) a first ion selective membrane; iii) a second ionselective membrane, wherein the first and second ion selective membranesdivide the volume of the first insulated container into a firsthydraulically isolated section, a second hydraulically isolated sectionand a third hydraulically isolated section, wherein the thirdhydraulically isolated section is located between the first and thesecond ion selective membranes, and wherein the third hydraulicallyisolated section serves as a first ion sink allowing for the formationof new chemical compounds; iv) a first electrode secured within thefirst hydraulically isolated section, wherein the first electrode is alow electrical capacitance electrode which allows the occurrence ofelectrode reactions; and v) a second electrode secured within the secondhydraulically isolated section, wherein the second electrode is an EDLCelectrode; b) a second cell comprising: i) a second insulated container;ii) a third ion selective membrane; iii) a fourth ion selectivemembrane, wherein the third and fourth ion selective membranes dividethe volume of the second insulated container into a fourth hydraulicallyisolated section, a fifth hydraulically isolated section and a sixthhydraulically isolated section, wherein the sixth hydraulically isolatedsection is located between the third and the fourth ion selectivemembranes, and wherein the sixth hydraulically isolated section servesas a second ion sink allowing for the formation of new chemicalcompounds; iv) a third electrode secured within the fourth hydraulicallyisolated section, wherein the third electrode is a low electricalcapacitance electrode which allows the occurrence of electrodereactions; and v) a fourth electrode secured within the fifthhydraulically isolated section, wherein the fourth electrode is an EDLCelectrode; c) a first electric current supply source for applying anelectric potential difference between the first electrode and the secondelectrode; and d) a second electric current supply source for applyingan electric potential difference between the third electrode and thefourth electrode.
 11. The apparatus of claim 10, wherein each of the ionselective membranes allows the passage of ions of the same polarity asthe charge applied to the electrode in its related hydraulicallyisolated section.
 12. The apparatus of claim 10, wherein the first ionselective membrane is an anion selective membrane, the second ionselective membrane is a cation selective membrane, the third ionselective membrane is a cation selective membrane, and the fourth ionselective membrane is an anion selective membrane.
 13. A process forseparation and selective recomposition of ions, the process comprising:a) providing a first cell comprising a first insulated container, afirst ion selective membrane, and a second ion selective membrane,wherein the first and second ion selective membranes divide the volumeof the first insulated container into a first hydraulically isolatedsection, a second hydraulically isolated section and a thirdhydraulically isolated section, wherein the third hydraulically isolatedsection is located between the first and the second ion selectivemembranes; b) providing a second cell comprising a second insulatedcontainer, a third ion selective membrane, and a fourth ion selectivemembrane, wherein the third and fourth ion selective membranes dividethe volume of the second insulated container into a fourth hydraulicallyisolated section, a fifth hydraulically isolated section and a sixthhydraulically isolated section, wherein the sixth hydraulically isolatedsection is located between the third and the fourth ion selectivemembranes; c) providing a first electrolyte solution in the firsthydraulically isolated section, a second electrolyte solution in thesecond hydraulically isolated section, a third electrolyte solution inthe fourth hydraulically isolated section, and a fourth electrolytesolution in the fifth hydraulically isolated section, wherein eachelectrolyte solution comprises positive ions and negative ions; d)separating the positive ions from the negative ions in each of thefirst, second, third, and fourth electrolyte solutions, whereinseparating comprises the steps of: i) placing a first EDLC electrodeinside the first electrolyte solution; ii) placing a second EDLCelectrode inside the second electrolyte solution; iii) placing a thirdEDLC electrode inside the third electrolyte solution; iv) placing afourth EDLC electrode inside the fourth electrolyte solution; and v)applying an electric potential difference between the first EDLCelectrode and the second EDLC electrode and between the third EDLCelectrode and the fourth EDLC electrode, such that two capacitors inseries are formed in each of the first, second, third and fourthelectrolyte solutions, wherein each of the two capacitors in seriescomprises: 1) an inner internal capacitor formed between the EDLCelectrode and the ions collected on and in close proximity to the EDLCelectrode; and 2) an outer internal capacitor formed at the outerperimeter of the electrolyte solution, wherein the formation of theouter internal capacitor in each of the first, second, third and fourthelectrolyte solutions leads to capacitive collection, concentration andvoltage buildup of excess charges on the outer perimeters of the first,second, third and fourth electrolyte solutions; e) electrically drawingthe ions out of each of the first, second, third and fourth electrolytesolutions as oppositely charged ion streams, wherein each of thepositive and negative ion streams is generated in a continuous fashionand is selectively drawn through the ion selective membrane selective tothe ion stream, and wherein the polarity of charges applied to the firstEDLC electrode and the fourth EDLC electrode are the same and thepolarity of the charges applied to the second EDLC electrode and thethird EDLC electrode are the same; f) pooling the ion stream from thefirst electrolyte solution and the oppositely charged ion stream fromthe second electrolyte solution into the third hydraulically isolatedsection, wherein the third hydraulically isolated section serves as afirst ion sink allowing for the formation of new chemical compounds; g)pooling the ion stream from the third electrolyte solution and theoppositely charged ion stream from the fourth electrolyte solution intothe sixth hydraulically isolated section, wherein the sixthhydraulically isolated section serves as a second ion sink allowing forthe formation of new chemical compounds; h) thereafter switching thelocation of the EDLC electrodes from the first cell and the second cellbefore occurrence of reactions at the EDLC electrodes, the step ofswitching the EDLC electrodes from the first cell to the second cellcomprising: i) removing the first, second, third and fourth EDLCelectrodes from their respective first, second, third and fourthelectrolyte solutions; ii) placing the first EDLC electrode in the thirdelectrolyte solution; iii) placing the second EDLC electrode in thefourth electrolyte solution; iv) placing the third EDLC electrode in thefirst electrolyte solution; and v) placing the fourth EDLC electrode inthe second electrolyte solution.
 14. The process of claim 13, furthercomprising repeating the steps of (d)(v) through (h)(v), therebyproviding continuous production of the new chemical compounds in thefirst and second ion sinks.
 15. The process of claim 13, wherein each ofthe ion selective membranes allows the passage of ions of the samepolarity as the charge applied to the electrode in its relatedhydraulically isolated section.
 16. The process of claim 13, wherein thefirst ion selective membrane is an anion selective membrane, the secondion selective membrane is a cation selective membrane, the third ionselective membrane is a cation selective membrane, and the fourth ionselective membrane is an anion selective membrane.
 17. A process forseparation and selective recomposition of ions, the process comprising:a) providing a first cell comprising a first insulated container, afirst ion selective membrane, and a second ion selective membrane,wherein the first and second ion selective membranes divide the volumeof the first insulated container into a first hydraulically isolatedsection, a second hydraulically isolated section and a thirdhydraulically isolated section, wherein the third hydraulically isolatedsection is located between the first and the second ion selectivemembranes; b) providing a second cell comprising a second insulatedcontainer, a third ion selective membrane, and a fourth ion selectivemembrane, wherein the third and fourth ion selective membranes dividethe volume of the second insulated container into a fourth hydraulicallyisolated section, a fifth hydraulically isolated section and a sixthhydraulically isolated section, wherein the sixth hydraulically isolatedsection is located between the third and the fourth ion selectivemembranes; c) providing a sodium hydroxide solution in the firsthydraulically isolated section, an ammonium chloride solution in thesecond hydraulically isolated section, a sulfuric acid solution in thefourth hydraulically isolated section, and an ammonium chloride solutionin the fifth hydraulically isolated section; d) separating the positivesodium ions from the negative hydroxide ions in the sodium hydroxidesolution in the first hydraulically isolated section, and the positiveammonium ions from the negative chloride ions in the ammonium chloridesolution in the second hydraulically isolated section, whereinseparating comprises the steps of: i) placing a low capacitanceelectrode inside the sodium hydroxide solution in the firsthydraulically isolated section; ii) placing an EDLC electrode inside theammonium chloride solution in the second hydraulically isolated section;iii) placing a low capacitance electrode inside the sulfuric acidsolution in the fourth hydraulically isolated section; iv) placing anEDLC electrode inside the ammonium chloride solution in the fifthhydraulically isolated section; and v) applying an electric potentialdifference via a first current supply source between the low capacitanceelectrode inside the sodium hydroxide solution in the firsthydraulically isolated section and the EDLC electrode inside theammonium chloride solution in the second hydraulically isolated section,such that a stream of negative hydroxide ions flows through the firstion selective membrane and a stream of positive ammonium ions flowsthrough the second ion selective membrane; vi) applying an electricpotential difference via a second current supply source between the lowcapacitance electrode inside the sulfuric acid solution in the fourthhydraulically isolated section and the EDLC electrode inside theammonium chloride solution in the fifth hydraulically isolated section,such that a stream of positively charged hydrogen ions flows through thethird ion selective membrane and a stream of negatively charged chlorineions flows through the fourth ion selective membrane; e) pooling thestream of negative hydroxide ions flowing through the first ionselective membrane and the stream of positive ammonium ions flowingthrough the second ion selective membrane into the third hydraulicallyisolated section, wherein the third hydraulically isolated sectionserves as a first ion sink allowing for the formation of ammoniumhydroxide; f) pooling the stream of positively charged hydrogen ionsflowing through the third ion selective membrane and the stream ofnegatively charged chlorine ions flowing through the fourth ionselective membrane into the sixth hydraulically isolated section,wherein the sixth hydraulically isolated section serves as a second ionsink allowing for the formation of hydrochloric acid. g) thereafterswitching the location of the EDLC electrodes from the secondhydraulically isolated section and the fifth hydraulically isolatedsection before occurrence of redox reactions at the EDLC electrodes, thestep of switching the EDLC electrodes from the second hydraulicallyisolated section and the fifth hydraulically isolated sectioncomprising: i) removing the EDLC electrodes from their respective secondand fifth hydraulically isolated sections; ii) placing the EDLCelectrode from the second hydraulically isolated section into the fifthhydraulically isolated section; and iii) placing the EDLC electrode fromthe fifth hydraulically isolated section into the second hydraulicallyisolated section.
 18. The process of claim 17, further comprisingrepeating the steps of (d)(v) through (g)(iii), thereby providingcontinuous production of the ammonium hydroxide in the first ion sinkand hydrochloric acid in the second ion sink.